Blends of lubricant basestocks with polyol esters

ABSTRACT

A lubricating composition is provided comprising a polyol ester which is the reaction product of a neopolyol with linear or branched monocarboxylic acids and mixtures thereof having from 1 to about 25 carbon atoms and a natural or GTL oil of lubricating viscosity and mixtures thereof and wherein the weight ratio of the ester to oil will be sufficient to provide a composition having a viscosity less than the individual viscosities of the ester and oil.

This application claims priority of Provisional Application 60/786,511 filed Mar. 28, 2006.

FIELD OF THE INVENTION

The present invention relates to blends of lubricant basestocks with polyol esters. More particularly, the invention relates to such blends in which the blends have a viscosity lower than the viscosity of the individual components.

BACKGROUND OF THE INVENTION

Lubricants in commercial use today are composed of a variety of natural and synthetic basestocks and performance enhancing additives which are selected depending upon their intended application. The natural basestocks typically include vegetable and mineral oils. The synthetic basestocks typically include polyalpha olefins and polyol esters. These natural and synthetic basestocks may be used alone or blended and formulated into a lubricating composition.

Basestocks may be blended for any of a variety of reasons. Typically blending is performed to alter one or more properties such as viscosity, viscosity index, stability, biodegradability and the like which are inherent to a single basestock composition.

The viscosities of binary mixtures have been investigated for many decades, and a number of semi-empirical or empirical equations have been developed to describe them. One of the most commonly used relationships is the Arrhenius equation:

log η=x log η₁+(1−x)log η₂

where η₁ and η₂ are the viscosities of components 1 and 2 and x is the fraction of component 1. If the viscosities of components 1 and 2 are the same, i.e., η₁=η₂, then it follows that the viscosity η of the mixture would be expected to be the same, i.e., η=η₁=η₂.

As is known, the Arrhenius equation is not applicable to the cases of associated solutions such as methanol and water. In such instances, there are many examples where the viscosity of the mixture is higher than the individual components. There are only a few cases that have been observed, however, where the viscosity of a mixture was lower than the individual components.

The present inventors have demonstrated that an unexpected, synergistic effect occurs when certain polyol esters are blended with either a natural or gas-to-liquids (GTL) basestock. Thus, blends of the invention comprise lube basestocks that have a viscosity lower than the viscosity of the individual components.

SUMMARY OF THE INVENTION

Accordingly, there is provided a lubricating composition comprising a polyol ester which is the reaction product of a neopolyol with linear or branched monocarboxylic acids and mixtures thereof having from 1 to about 25 carbon atoms and a natural or GTL oil of lubricating viscosity and mixtures thereof and wherein the weight ratio of the ester to oil will be a ratio sufficient to provide a composition having a viscosity less than the individual viscosities of the ester and oil.

BRIEF DESCRIPTION OF THE DRAWINGS

FIGS. 1 to 10 are graphs of the experimental data illustrating the invention.

DETAILED DESCRIPTION OF THE INVENTION

The esters in the compositions of the invention are comprised of neopolyols and one or more monocarboxylic acids. Examples of suitable neopolyols are neopentylglycol, trimethylolpropane, monopentaerythritol, technical grade pentaerythritol, dipentaerythiritol and the like. Examples of suitable monocarboxylic acids range from formic acid through long chain acids of up to about 25 carbon atoms. Thus the monocarboxylic acids are linear or branched acids having from 1 to about 25 carbon atoms. Neopolyol esters comprised of a mixture of monocarboxylic acids is preferred in the practice of the invention.

The polyol esters suitable for use in the compositions of the invention may have from 0 up to about 1 unconverted hydroxyl group per molecule. The typical viscosities for the polyol ester range from 2 cSt to 30 cSt at 100 C.

The preparation of such esters is well known in the art and esters are commercially available.

The oil of lubricating viscosity used in the invention is selected from natural oils, especially mineral oils and GTL oils.

Hydroisomerate/isodewaxate base stocks and base oils include base stocks and base oils derived from one or more GTL materials, slack waxes, natural waxes and the waxy stocks such as gas oils, waxy fuels hydrocracker bottoms, waxy raffinate, hydrocrackate, thermal crackates, or other mineral or non-mineral oil derived waxy materials, and mixtures of such base stocks.

GTL materials are materials that are derived via one or more synthesis, combination, transformation, rearrangement, and/or degradation/deconstructive processes from gaseous carbon-containing compounds, hydrogen-containing compounds, and/or elements as feedstocks such as hydrogen, carbon dioxide, carbon monoxide, water, methane, ethane, ethylene, acetylene, propane, propylene, propyne, butane, butylenes, and butynes. GTL base stocks and base oils are GTL materials of lubricating viscosity that are generally derived from hydrocarbons, for example waxy synthesized hydrocarbons, that are themselves derived from simpler gaseous carbon-containing compounds, hydrogen-containing compounds and/or elements as feedstocks. GTL base stocks and base oils include wax isomerates, comprising, for example, hydroisomerized or isodewaxed synthesized waxy hydrocarbons, hydroisomerized or isodewaxed Fischer-Tropsch (F-T) material (i.e., hydrocarbons, waxy hydrocarbons, waxes and possible analogous oxygenates), preferably hydroisomerized or isodewaxed F-T waxy hydrocarbons or hydroisomerized or isodewaxed F-T waxes, hydro-isomerized or isodewaxed synthesized waxes, or mixtures thereof The term GTL base stocks and base oil further encompass the aforesaid base stock and base oils in combination with other hydroisomerized or isodewaxed materials comprising for example, hydroisomerized or isodewaxed mineral/petroleum-derived hydrocarbons, hydroisomerized or isodewaxed waxy hydrocarbons, or mixtures thereof, derived from different feed materials including, for example, waxy distillates such as gas oils, waxy hydrocracked hydrocarbons, lubricating oils, high pour point polyalphaolefins, foots oil, normal alpha olefin waxes, slack waxes, deoiled waxes, and microcrystalline waxes.

GTL base stocks and base oils derived from GTL materials, especially, hydroisomerized/isodewaxed F-T material derived base stocks and base oils, and other hydroisomerized/isodewaxed wax derived base stocks and base oils, such as wax isomerates are characterized typically as having kinematic viscosities at 100° C. of from about 2 cSt to about 50 cSt, preferably from about 3 cSt to about 30 cSt, more preferably from about 3.5 cSt to about 25 cSt, as exemplified by a GTL base stock derived by the isodewaxing of F-T wax, which has a kinematic viscosity of about 4 cSt at 100° C. and a viscosity index of about 130 or greater. Reference herein to Kinematic viscosity refers to a measurement made by ASTM method D445.

GTL base stocks and base oils derived from GTL materials, especially hydroisomerized/isodewaxed F-T material derived base stocks and base oils, and other hydroisomerized/isodewaxed wax-derived base stocks and base oils, such as wax hydroisomerates/isodewaxates, which are components of this invention are further characterized typically as having pour points of about −5° C. or lower, preferably about −10° C. or lower, more preferably about −15° C. or lower, still more preferably about −20° C. or lower, and under some conditions may have advantageous pour points of about −25° C. or lower, with useful pour points of about −30° C. to about −40° C. or lower. If necessary, a separate dewaxing step may be practiced to achieve the desired pour point. References herein to pour point refer to measurement made by ASTM D97 and similar automated versions.

The GTL base stocks and base oils derived from GTL materials, especially hydroisomerized/isodewaxed F-T material derived base stocks and base oils, and other hydroisomerized/isodewaxed wax-derived base stocks and base oils, such as wax isomerate/isodewaxate which are components of this invention are also characterized typically as having viscosity indices of 80 or greater, preferably 100 or greater, and more preferably 120 or greater. Additionally, in certain particular instances, viscosity index of these base stocks may be preferably 130 or greater, more preferably 135 or greater, and even more preferably 140 or greater. For example, GTL base stocks and base oils that derived from GTL materials preferably F-T materials especially F-T wax generally have a viscosity index of 130 or greater. References herein to viscosity index refer to ASTM method D2270.

In addition, the GTL base stocks and base oils are typically highly paraffinic (>90 wt % saturates), and may contain mixtures of monocycloparaffins and multicycloparaffins in combination with non-cyclic isoparaffins. The ratio of the naphthenic (i.e., cycloparaffin) content in such combinations varies with the catalyst and temperature used. Further, GTL base stocks and base oils typically have very low sulfur and nitrogen content, generally containing less than about 10 ppm, and more typically less than about 5 ppm of each of these elements. The sulfur and nitrogen content of GTL base stock and base oil obtained by the hydroisomerization/isodewaxing of F-T material, especially F-T wax is essentially nil.

Useful compositions of GTL base stocks and base oils, hydro-isomerized or isodewaxed F-T material derived base stocks and base oils, and wax-derived hydroisomerized/isodewaxed base stocks and base oils, such as wax isomerates/isodewates, are recited in U.S. Pat. Nos. 6,080,301; 6,090,989, and 6,165,949 for example.

Wax isomerate/isodewaxate base stocks and base oils derived from waxy feeds which are also suitable for use in this invention, are paraffinic fluids of lubricating viscosity derived from hydroisomerized or isodewaxed waxy feedstocks of mineral or natural source origin, e.g., feedstocks such as one or more of gas oils, slack wax, waxy fuels hydrocracker bottoms, hydrocarbon raffinates, natural waxes, hyrocrackates, thermal crackates or other suitable mineral or non-mineral oil derived waxy materials, linear or branched hydro-carbyl compounds with carbon number of about 20 or greater, preferably about 30 or greater, and mixtures of such isomerate/isodewaxate base stocks and base oils.

As used herein, the following terms have the indicated meanings:

“paraffinic” material: any saturated hydrocarbons, such as alkanes. Paraffinic materials may include linear alkanes, branched alkanes (iso-paraffins), cycloalkanes (cycloparaffins; mono-ring and/or multi-ring), and branched cycloalkanes;

“wax”: hydrocarbonaceous material having a high pour point, typically existing as a solid at room temperature, at about 15° C. to 25° C., and consisting predominantly of paraffinic materials;

“hydroprocessing”: a refining process in which a feedstock is heated with hydrogen at high temperature and under pressure, commonly in the presence of a catalyst, to remove and/or convert less desirable components and to produce an improved product;

“hydrotreating”: a catalytic hydrogenation process that converts sulfur- and/or nitrogen-containing hydrocarbons into hydrocarbon products with reduced sulfur and/or nitrogen content, and which generates hydrogen sulfide and/or ammonia (respectively) as byproducts; similarly, oxygen containing hydrocarbons can also be reduced to hydrocarbons and water;

“hydrodewaxing” (or catalytic dewaxing): a catalytic process in which normal paraffins and/or waxy hydrocarbons are converted by cracking/fragmentation into lower molecular weight species, and/or by rearrangement/isomerization into more branched iso-paraffins;

“hydroisomerization” (or isodewaxing): a catalytic process in which normal paraffins and/or slightly branched iso-paraffins are converted by rearrangement/isomerization into more branched iso-paraffins;

“hydrocracking”: a catalytic process in which hydrogenation accompanies the cracking/fragmentation of hydrocarbons, e.g., converting heavier hydrocarbons into lighter hydrocarbons, or converting aromatics and/or cycloparaffins (naphthenes) into non-cyclic branched paraffins.

As previously indicated, wax isomerate base stock and base oils suitable for use as the necessary components in the present invention, can be derived from other waxy feeds such as slack wax.

Slack wax is the wax recovered from petroleum oils by solvent or autorefrigerative dewaxing. Solvent dewaxing employs chilled solvent such as methyl ethyl ketone (MEK), methyl isobutyl ketone (MIBK), mixtures of MEK/MIBK, mixtures of MEK and toluene, while autorefrigerative dewaxing employs pressurized, liquefied low boiling hydrocarbons such as propane or butane.

Slack waxes, being secured from petroleum oils, may contain sulfur and nitrogen containing compounds. Such heteroatom compounds must be removed by hydrotreating (and not hydrocracking), as for example by hydrodesulfurization (HDS) and hydrodenitrogenation (HDN) so as to avoid subsequent poisoning/deactivation of the hydroisomerization catalyst.

In a preferred embodiment, the GTL material is a F-T material (i.e., hydrocarbons, waxy hydrocarbons, wax). A slurry F-T synthesis process may be beneficially used for synthesizing the feed from CO and hydrogen and particularly one employing a F-T catalyst comprising a catalytic cobalt component to provide a high alpha for producing the more desirable higher molecular weight paraffins. This process is also well known to those skilled in the art.

In a F-T synthesis process, a synthesis gas comprising a mixture of H₂ and CO is catalytically converted into hydrocarbons and preferably liquid hydrocarbons. The mole ratio of the hydrogen to the carbon monoxide may broadly range from about 0.5 to 4, but which is more typically within the range of from about 0.7 to 2.75 and preferably from about 0.7 to 2.5. As is well known, F-T synthesis processes include processes in which the catalyst is in the form of a fixed bed, a fluidized bed or as a slurry of catalyst particles in a hydrocarbon slurry liquid. The stoichiometric mole ratio for a F-T synthesis reaction is 2.0, but there are many reasons for using other than a stoichiometric ratio as those skilled in the art know. In a cobalt slurry hydrocarbon synthesis process the feed mole ratio ofthe H₂ to CO is typically about 2.1/1. The synthesis gas comprising a mixture of H₂ and CO is bubbled up into the bottom of the slurry and reacts in the presence of the particulate F-T synthesis catalyst in the slurry liquid at conditions effective to form hydrocarbons, a portion of which are liquid at the reaction conditions and which comprise the hydrocarbon slurry liquid. The synthesized hydrocarbon liquid is separated from the catalyst particles as filtrate by means such as filtration, although other separation means such as centrifugation can be used. Some of the synthesized hydrocarbons pass out the top of the hydrocarbon synthesis reactor as vapor, along with unreacted synthesis gas and other gaseous reaction products. Some of these overhead hydrocarbon vapors are typically condensed to liquid and combined with the hydrocarbon liquid filtrate. Thus, the initial boiling point of the filtrate may vary depending on whether or not some of the condensed hydrocarbon vapors have been combined with it. Slurry hydrocarbon synthesis process conditions vary somewhat depending on the catalyst and desired products. Typical conditions effective to form hydrocarbons comprising mostly C₅₊ paraffins, (e.g., C₅₊-C₂₀₀) and preferably C₁₀₊ paraffins, in a slurry hydrocarbon synthesis process employing a catalyst comprising a supported cobalt component include, for example, temperatures, pressures and hourly gas space velocities in the range of from about 320-850° F., 80-600 psi and 100-40,000 V/hr/V, expressed as standard volumes of the gaseous CO and H₂ mixture (0° C., 1 atm) per hour per volume of catalyst, respectively. It is preferred that the hydrocarbon synthesis reaction be conducted under conditions in which limited or no water gas shift reaction occurs and more preferably with no water gas shift reaction occurring during the hydrocarbon synthesis. It is also preferred to conduct the reaction under conditions to achieve an alpha of at least 0.85, preferably at least 0.9 and more preferably at least 0.92, so as to synthesize more of the more desirable higher molecular weight hydrocarbons. This has been achieved in a slurry process using a catalyst containing a catalytic cobalt component. Those skilled in the art know that by alpha is meant the Schultz-Flory kinetic alpha. While suitable F-T reaction types of catalyst comprise, for example, one or more Group VIII catalytic metals such as Fe, Ni, Co, Ru and Re, it is preferred that the catalyst comprise a cobalt catalytic component. In one embodiment the catalyst comprises catalytically effective amounts of Co and one or more of Re, Ru, Fe, Ni, Th, Zr, Hf, U, Mg and La on a suitable inorganic support material, preferably one which comprises one or more refractory metal oxides. Preferred supports for Co containing catalysts comprise titania, particularly. Useful catalysts and their preparation are known and illustrative, but nonlimiting examples may be found, for example, in U.S. Pat. Nos. 4,568,663; 4,663,305; 4,542,122; 4,621,072 and 5,545,674.

As set forth above, the waxy feed from which a preferred base stock is derived comprises mineral wax or other natural source wax, especially slack wax, or waxy F-T material, referred to as F-T wax. F-T wax preferably has an initial boiling point in the range of from 650-750° F. and preferably continuously boils up to an end point of at least 1050° F. A narrower cut waxy feed may also be used during the hydroisomerization. A portion of the n-paraffin waxy feed is converted to lower boiling isoparaffinic material. Hence, there must be sufficient heavy n-paraffin material to yield an isoparaffin containing isomerate boiling in the lube oil range. If catalytic dewaxing is also practiced, some of the isomerate will also be converted to lower boiling material during the dewaxing. Hence, it is preferred that the end boiling point of the waxy feed be above 1050° F. (1050° F.+).

The waxy feed preferably comprises the entire 650-750° F.+ fraction formed by the hydrocarbon synthesis process, with the initial cut point between 650° F. and 750° F. being determined by the practitioner and the end point, preferably above 1050° F., determined by the catalyst and process variables employed by the practitioner for the synthesis. Waxy feeds may be processed as the entire fraction or as subsets of the entire fraction prepared by distillation or other separation techniques. The waxy feed also typically comprises more than 90 wt %, generally more than 95 wt % and preferably more than 98 wt % paraffinic hydrocarbons, most of which are normal paraffins. It has negligible amounts of sulfur and nitrogen compounds (e.g., less than 1 wppm of each), with less than 2,000 wppm, preferably less than 1,000 wppm and more preferably less than 500 wppm of oxygen, in the form of oxygenates. Waxy feeds having these properties and useful in the process of the invention have been made using a slurry F-T process with a catalyst having a catalytic cobalt component, as previously indicated.

The process of making the lubricant oil base stocks from waxy stocks, e.g., slack wax or F-T wax, may be characterized as a hydrodewaxing process. If slack waxes are used as the feed, they may need to be subjected to a preliminary hydrotreating step under conditions already well known to those skilled in the art to reduce (to levels that would effectively avoid catalyst poisoning or deactivation) or to remove sulfur- and nitrogen-containing lo compounds which would otherwise deactivate the hydroisomerization/ hydrodewaxing catalyst used in subsequent steps. If F-T waxes are used, such preliminary treatment is not required because, as indicated above, such waxes have only trace amounts (less than about 10 ppm, or more typically less than about 5 ppm to nil) of sulfur or nitrogen compound content. However, some hydrodewaxing catalyst fed F-T waxes may benefit from removal of oxygenates while others may benefit from oxygenates treatment. The hydrodewaxing process may be conducted over a combination of catalysts, or over a single catalyst. Conversion temperatures range from about 150° C. to about 500° C. at pressures ranging from about 500 to 20,000 kPa. This process may be operated in the presence of hydrogen, and hydrogen partial pressures range from about 600 to 6000 kPa. The ratio of hydrogen to the hydrocarbon feedstock (hydrogen circulation rate) typically range from about 10 to 3500 n.l.l.⁻¹ (56 to 19,660 SCF/bbl) and the space velocity of the feedstock typically ranges from about 0.1 to 20 LHSV, preferably 0.1 to 10 LHSV.

Following any needed hydridenitrogenation or hydrodesulfurization, the hydroprocessing used for the production of base stocks from such waxy feeds may use an amorphous hydrocracking/hydroisomerization catalyst, such as a lube hydrocracking (LHDC) catalysts, for example catalysts containing Co, Mo, Ni, W, Mo, etc., on oxide supports, e.g., alumina, silica, silica/alumina, or a crystalline hydrocracking/hydroisomerization catalyst, preferably a zeolitic catalyst.

Other isomerization catalysts and processes for hydrocracking/hydroisomerized/isodewaxing GTL materials and/or waxy materials to base stock or base oil are described, for example, in U.S. Pat. Nos. 2,817,693; 4,900,407; 4,937,399; 4,975,177; 4,921,594; 5,059,299; 5,200,382; 5,516,740; 5,182,248; 5,290,426; 5,580,442; 5,976,351; 5,935,417; 5,885,438; 5,965,475; 6,190,532;6,375,830; 6,332,974; 6,103,099; 6,025,305; 6,080,301;6,096,940; 6,620,312; 6,676,827; 6,383,366; 6,475,960; 5,059,299; 5,977,425; 5,935,416; 4,923,588; 5,158,671; and 4,897,178; EP 0324528 (B1), EP 0532116 (B1), EP 0532118 (B1), EP 0537815 (B1), EP 0583836 (B2), EP 0666894 (B2), EP 0668342 (B1), EP 0776959 (A3), WO 97/031693 (A1), WO 02/064710 (A2), WO 02/064711 (A1), WO 02/070627 (A2), WO 02/070629 (A1), WO 03/033320 (A1) as well as in British Patents 1,429,494; 1,350,257; 1,440,230; 1,390,359; WO 99/45085 and WO 99/20720. Particularly favorable processes are described in European Patent Applications 464546 and 464547. Processes using F-T wax feeds are described in U.S. Pat. Nos. 4,594,172; 4,943,672; 6,046,940; 6,475,960; 6,103,099; 6,332,974; and 6,375,830.

Hydrocarbon conversion catalysts useful in the conversion of the n-paraffin waxy feedstocks disclosed herein to form the isoparaffinic hydro-carbon base oil are zeolite catalysts, such as ZSM-5, ZSM-11, ZSM-23, ZSM-35, ZSM-12, ZSM-38, ZSM-48, offretite, ferrierite, zeolite beta, zeolite theta, zeolite alpha, as disclosed in U.S. Pat. No. 4,906,350. These catalysts are used in combination with Group VIII metals, in particular palladium or platinum. The Group VIII metals may be incorporated into the zeolite catalysts by conventional techniques, such as ion exchange.

In one embodiment, conversion of the waxy feedstock may be conducted over a combination of Pt/zeolite beta and Pt/ZSM-23 catalysts in the presence of hydrogen. In another embodiment, the process of producing the lubricant oil base stocks comprises hydroisomerization and dewaxing over a single catalyst, such as Pt/ZSM-35. In yet another embodiment, the way feed can be fed over Group VIII metal loaded ZSM-48, preferably Group VIII noble metal loaded ZSM-48, more preferably Pt/ZSM-48 in either one stage or two stages. In any case, useful hydrocarbon base oil products may be obtained. Catalyst ZSM-48 is described in U.S. Pat. No. 5,075,269, the disclosure of which is incorporated herein by reference in its entirety. The use of the Group VIII metal loaded ZSM-48 family of catalysts in the isodewaxing of the waxy feedstock eliminates the need for any subsequent, separate dewaxing step, and is preferred.

A dewaxing step, when needed, may be accomplished using either well known solvent or catalytic dewaxing processes and either the entire hydroisomerate or the 650-750° F.+ fraction may be dewaxed, depending on the intended use of the 650-750° F.− material present, if it has not been separated from the higher boiling material prior to the dewaxing. In solvent dewaxing, the hydroisomerate may be contacted with chilled solvents such as acetone, methyl ethyl ketone (MEK), methyl isobutyl ketone (MIBK), mixtures of MEK/MIBK, or mixtures of MEK/toluene and the like, and further chilled to precipitate out the higher pour point material as a waxy solid which is then separated from the solvent-containing lube oil fraction which is the raffinate. The raffinate is typically further chilled in scraped surface chillers to remove more wax solids. Low molecular weight hydrocarbons, such as propane, are also used for dewaxing, in which the hydroisomerate is mixed with liquid propane, a least a portion of which is flashed off to chill down the hydroisomerate to precipitate out the wax. The wax is separated from the raffinate by filtration, membrane separation or centrifugation. The solvent is then stripped out of the raffinate, which is then fractionated to produce the preferred base stocks useful in the present invention. Also well known is catalytic dewaxing, in which the hydroisomerate is reacted with hydrogen in the presence of a suitable dewaxing catalyst at conditions effective to lower the pour point of the hydroisomerate. Catalytic dewaxing also converts a portion of the hydroisomerate to lower boiling materials, in the boiling range, for example, 650-750° F.−, which are separated from the heavier 650-750° F.+ base stock fraction and the base stock fraction fractionated into two or more base stocks. Separation of the lower boiling material may be accomplished either prior to or during fractionation of the 650-750° F.+ material into the desired base stocks.

Any dewaxing catalyst which will reduce the pour point of the hydroisomerate and preferably those which provide a large yield of lube oil base stock from the hydroisomerate may be used. These include shape selective molecular sieves which, when combined with at least one catalytic metal component, have been demonstrated as useful for dewaxing petroleum oil fractions and include, for example, ferrierite, mordenite, ZSM-5, ZSM-11, ZSM-23, ZSM-35, ZSM-22 also known as theta one or TON, and the silicoaluminophosphates known as SAPO's. A dewaxing catalyst which has been found to be unexpectedly particularly effective comprises a noble metal, preferably Pt, composited with H-mordenite. The dewaxing may be accomplished with the catalyst in a fixed, fluid or slurry bed. Typical dewaxing conditions include a temperature in the range of from about 400-600° F., a pressure of 500-900 psig, H₂ treat rate of 1500-3500 SCF/B for flow-through reactors and LHSV of 0.1-10, preferably 0.2-2.0. The dewaxing is typically conducted to convert no more than 40 wt % and preferably no more than 30 wt % of the hydroisomerate having an initial boiling point in the range of 650-750° F. to material boiling below its initial boiling point.

GTL base stocks and base oils, hydroisomerized or isodewaxed wax-derived base stocks and base oils, have a beneficial kinematic viscosity advantage over conventional Group II and Group III base stocks and base oils, and so may be very advantageously used with the instant invention. Such GTL base stocks and base oils can have significantly higher kinematic viscosities, up to about 20-50 cSt at 100° C., whereas by comparison commercial Group II base oils can have kinematic viscosities, up to about 15 cSt at 100° C., and commercial Group III base oils can have kinematic viscosities, up to about 10 cSt at 100° C. The higher kinematic viscosity range of GTL base stocks and base oils, compared to the more limited kinematic viscosity range of Group II and Group III base stocks and base oils, in combination with the instant invention can is provide additional beneficial advantages in formulating lubricant compositions.

In the present invention the hydroisomerate isodewaxate oil can constitute all or part of the base stock oil.

One or more of these wax isomerate/isodewaxate base stocks and base oils can be used as such or in combination with the aforesaid GTL base stocks and base oils.

One or more of these waxy feed derived base stocks and base oils, derived from GTL materials and/or other waxy feed materials can similarly be used as such or further in combination with other base stock and base oils of mineral oil origin, natural oils and/or with other synthetic base oils.

The preferred base stocks or base oils derived form GTL materials and/or from waxy feeds are characterized as having predominantly paraffinic compositions and are further characterized as having high saturates levels, low-to-nil sulfur, low-to-nil nitrogen, low-to-nil aromatics, and are essentially water-white in color.

The hydroisomerate/isodewaxate can constitute from 5 to 100 wt %, preferably 40 to 100 wt %, more preferably 70 to 100 wt % by weight of the total of the base oil, the amount employed being left to the practitioner in response to the requirements of the finished lubricant.

Natural oil, other synthetic oils, and unconventional oils and mixtures thereof can be used unrefined, refined, or rerefined (the latter is also known as reclaimed or reprocessed oil). Unrefined oils are those obtained directly from a natural, synthetic or unconventional source and used without further purification. These include for example shale oil obtained directly from retorting operations, petroleum oil obtained directly from primary distillation, and ester oil obtained directly from an esterification process. Refined oils are similar to the oils discussed for unrefined oils except refined oils are subjected to one or more purification or transformation steps to improve at least one lubricating oil property. One skilled in the art is familiar with many purification or transformation processes. These processes include, for example, solvent extraction, secondary distillation, acid extraction, base extraction, filtration, percolation, hydrogenation, hydrorefining, and hydrofinishing. Rerefined oils are obtained by processes analogous to refined oils, but use an oil that has been previously used.

Groups I, II, III, IV and V are broad categories of base oil stocks developed and defined by the American Petroleum Institute (API Publication 1509; www.API.org) to create guidelines for lubricant base oils. Group I base stocks generally have a viscosity index of between about 80 to 120 and contain greater than about 0.03 wt % sulfur and less than about 90 wt % saturates. Group II base stocks generally have a viscosity index of between about 80 to 120, and contain less than or equal to about 0.03 wt % sulfur and greater than or equal to about 90 wt % saturates. Group III stock generally has a viscosity index greater than about 120 and contains less than or equal to about 0.03 wt % sulfur and greater than about 90 wt % saturates. Group IV includes polyalphaolefins (PAO). Group V base stocks include base stocks not included in Groups I-IV. Table A summarizes properties of each of these five groups.

TABLE A Base Stock Properties Saturates Sulfur Viscosity Index Group I <90 wt % and/or >0.03 wt % and ≧80 and <120 Group II ≧90 wt % and ≦0.03 wt % and ≧80 and <120 Group III ≧90 wt % and ≦0.03 wt % and ≧120 Group IV Polyalphaolefins (PAO) Group V All other base oil stocks not included in Groups I, II, III, or IV

Natural oils include animal oils, vegetable oils (castor oil and lard oil, for example), and mineral oils. Animal and vegetable oils possessing favorable thermal oxidative stability can be used. Of the natural oils, mineral oils are preferred. Mineral oils vary widely as to their crude source, for example, as to whether they are paraffinic, naphthenic, or mixed paraffinic-naphthenic. Oils derived from coal or shale are also useful in the present invention. Natural oils vary also as to the method used for their production and purification, for example, their distillation range and whether they are straight run or cracked, hydrorefined, or solvent extracted.

Synthetic oils include hydrocarbon oils as well as non hydrocarbon oils. Synthetic oils can be derived from processes such as chemical combination (for example, polymerization, oligomerization, condensation, alkylation, acylation, etc.), where materials consisting of smaller, simpler molecular species are built up (i.e., synthesized) into materials consisting of larger, more complex molecular species. Synthetic oils include hydrocarbon oils such as polymerized and interpolymerized olefins (polybutylenes, polypropylenes, propylene isobutylene copolymers, ethylene-olefin copolymers, and ethylene-alphaolefin copolymers, for example). Polyalphaolefin (PAO) oil base stock is a commonly used synthetic hydrocarbon oil. By way of example, PAO's derived from C₈, C₁₀, C₁₂, C₁₄ olefins or mixtures thereof may be utilized. See U.S. Pat. Nos. 4,956,122; 4,827,064; and 4,827,073.

The PAO's, which are known materials and generally available on a major commercial scale from suppliers such as ExxonMobil Chemical Company, Chevron, BP-Amoco, and others, typically vary in number average molecular weight from about 250 to about 3000, or higher, and PAO's may be made in kinematic viscosities up to about 100 cSt (100° C.), or higher. In addition, higher viscosity PAO's are commercially available, and may be made in kinematic viscosities up to about 3000 cSt (100° C.), or higher. The PAO's are typically comprised of hydrogenated polymers or oligomers of alphaolefins which include, but are not limited to, about C₂ to about C₃₂ alphaolefins with about C₈ to about C₁₆ alphaolefins, such as 1-octene, 1-decene, 1-dodecene and the like, being preferred. The preferred polyalphaolefins are poly-1-octene, poly-1-decene and poly-1-dodecene and mixtures thereof and mixed olefin-derived polyolefins. However, the dimers of higher olefins in the range of about C₁₄ to C₁₈ may be used to provide low viscosity base stocks of acceptably low volatility. Depending on the viscosity grade and the starting oligomer, the PAO's may be predominantly trimers and tetramers of the starting olefins, with minor amounts of the higher oligomers, having a viscosity range of about 1.5 to 12 cSt.

PAO fluids may be conveniently made by the polymerization of an alphaolefin in the presence of a polymerization catalyst such as the Friedel-Crafts catalysts including, for example, aluminum trichloride, boron trifluoride or complexes of boron trifluoride with water, alcohols such as ethanol, propanol or butanol, carboxylic acids or esters such as ethyl acetate or ethyl propionate. For example the methods disclosed by U.S. Pat. No. 4,149,178 or U.S. Pat. No. 3,382,291 may be conveniently used herein. Other descriptions of PAO synthesis are found in the following U.S. Pat. Nos. 3,742,082; 3,769,363; 3,876,720; 4,239,930; 4,367,352; 4,413,156; 4,434,408; 4,910,355; 4,956,122; and 5,068,487. The dimers of the C₁₄ to C₁₈ olefins are described in U.S. Pat. No. 4,218,330.

Other useful synthetic lubricating base stock oils such as silicon-based oil or esters of phosphorus containing acids may also be utilized. For examples of other synthetic lubricating base stocks are the seminal work “Synthetic Lubricants”, Gunderson and Hart, Reinhold Publ. Corp., NY 1962, which is incorporated in its entirety.

In alkylated aromatic stocks such as mono- or poly-alkylbenzenes or mono- or poly-alkyl naphthalenes, the alkyl substituents are typically alkyl groups of about 8 to 25 carbon atoms, usually from about 10 to 18 carbon atoms and up to about three such substituents may be present, as described for the alkyl benzenes in ACS Petroleum Chemistry Preprint 1053-1058, “Poly n-Alkylbenzene Compounds: A Class of Thermally Stable and Wide Liquid Range Fluids”, Eapen et al, Phila. 1984. Tri-alkyl benzenes may be produced by the cyclodimerization of 1-alkynes of 8 to 12 carbon atoms as described in U.S. Pat. No. 5,055,626. Other alkylbenzenes are described in European Patent Application 168 534 and U.S. Pat. No. 4,658,072. Alkylbenzenes are used as lubricant base stocks and base oils, especially for low-temperature applications (arctic vehicle service and refrigeration oils) and in papermaking oils. They are commercially available from producers of linear alkylbenzenes (LABs) such as Vista Chem. Co., Huntsman Chemical Co., Chevron Chemical Co., and Nippon Oil Co. Linear alkylbenzenes typically have good low pour points and low temperature viscosities and VI values greater than about 100, together with good solvency for additives. Other alkylated aromatics which may be used when desirable are described, for example, in “Synthetic Lubricants and High Performance Functional Fluids”, Dressler, H., chap 5, (R. L. Shubkin (Ed.)), Marcel Dekker, NY, 1993.

Alkylene oxide polymers and interpolymers and their derivatives containing modified terminal hydroxyl groups obtained by, for example, esterification or etherification are useful synthetic lubricating oils. By way of example, these oils may be obtained by polymerization of ethylene oxide or propylene oxide, the alkyl and aryl ethers of these polyoxyalkylene polymers (methyl-polyisopropylene glycol ether having an average molecular weight of about 1000, diphenyl ether of polyethylene glycol having a molecular weight of about 500-1000, and the diethyl ether of polypropylene glycol having a molecular weight of about 1000 to 1500, for example) or mono- and poly-carboxylic esters thereof (the acidic acid esters, mixed C₃₋₈ fatty acid esters, or the C₁₃Oxo acid diester of tetraethylene glycol, for example).

Esters comprise a useful base stock. Additive solvency and seal compatibility characteristics may be secured by the use of esters such as the esters of dibasic acids with monoalkanols and the polyol esters of mono-carboxylic acids. Esters of the former type include, for example, the esters of dicarboxylic acids such as phthalic acid, succinic acid, alkyl succinic acid, alkenyl succinic acid, maleic acid, azelaic acid, suberic acid, sebacic acid, fumaric acid, adipic acid, linoleic acid dimer, malonic acid, alkyl malonic acid, alkenyl malonic acid, etc., with a variety of alcohols such as butyl alcohol, hexyl alcohol, dodecyl alcohol, 2-ethylhexyl alcohol, etc. Specific examples of these types of esters include dibutyl adipate, di(2-ethylhexyl) sebacate, di-n-hexyl fumarate, dioctyl sebacate, diisooctyl azelate, diisodecyl azelate, dioctyl phthalate, didecyl phthalate, etc.

Particularly useful synthetic esters are those full or partial esters which are obtained by reacting one or more polyhydric alcohols (preferably the hindered polyols such as the neopentyl polyols, e.g., neopentyl glycol, trimethylol ethane, 2-methyl-2-propyl-1,3-propanediol, trimethylol propane, pentaerythritol and dipentaerythritol) with alkanoic acids containing at least about 4 carbon atoms (preferably C₅ to C₃₀ acids such as saturated straight chain fatty acids including caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, arachic acid, and behenic acid, or the corresponding branched chain fatty acids or unsaturated fatty acids such as oleic acid).

Suitable synthetic ester components include the esters of trimethylol propane, trimethylol butane, trimethylol ethane, pentaerythritol and/or dipentaerythritol with one or more monocarboxylic acids containing from about 5 to about 10 carbon atoms.

Silicon-based oils are another class of useful synthetic lubricating oils. These oils include polyalkyl-, polyaryl-, polyalkoxy-, and polyaryloxy-siloxane oils and silicate oils. Examples of suitable silicon-based oils include tetraethyl silicate, tetraisopropyl silicate, tetra-(2-ethylhexyl)silicate, tetra-(4-methylhexyl) silicate, tetra-(p-tert-butylphenyl) silicate, hexyl-(4-methyl-2-pentoxy) disiloxane, poly(methyl) siloxanes, and poly-(methyl-2-mehtylphenyl) siloxanes.

Another class of synthetic lubricating oil is esters of phosphorous-containing acids. These include, for example, tricresyl phosphate, trioctyl phosphate, diethyl ester of decanephosphonic acid.

Another class of oils includes polymeric tetrahydrofurans, their derivatives, and the like.

Other useful fluids of lubricating viscosity include non-conventional or unconventional base stocks that have been processed, preferably catalytically, or synthesized to provide high performance lubrication characteristics.

The base stocks and/or base oils of this invention may be blended with effective amounts of one or more suitable additives to form lubricant compositions.

Examples of typical additives include, but are not limited to, oxidation inhibitors, antioxidants, dispersants, detergents, corrosion inhibitors, rust inhibitors, metal deactivators, anti-wear agents, extreme pressure additives, anti-seizure agents, pour point depressants, wax modifiers, viscosity index improvers, viscosity modifiers, viscosity index improvers, fluid-loss additives, seal compatibility agents, friction modifiers, lubricity agents, anti-staining agents, chromophoric agents, defoamants, demulsifiers, emulsifiers, densifiers, wetting agents, gelling agents, tackiness agents, colorants, and others. For a review of many commonly used additives, see Klamann in Lubricants and Related Products, Verlag Chemie, Deerfield Beach, Fla.; ISBN 0-89573-177-0. Reference is also made to “Lubricant Additives” by M. W. Ranney, published by Noyes Data Corporation of Parkridge, N.J. (1973).

The base stocks and /or base oils of this invention or their corresponding lubricant compositions may also be used as blending components with additional other base stocks and base oils of lubricating viscosity.

Finished lubricants comprise a lubricant base stock or base oil, plus at least one additive.

In general, the weight ratio of ester to oil in the compositions of the invention will be that sufficient to provide a composition having a viscosity less than the individual viscosities of the ester and oil. Typically, the weight ratio of ester to oil will be in the range of about 20:80 to about 80:20 although a range of about 40:60 to about 60:40 may be preferred.

In one aspect of the invention when the oil is a mineral oil, the ester and oil will be chosen from materials having the same or substantially the same viscosities. Indeed, the oils of lubricating viscosity may be blended to provide the requisite viscosity to match that of the ester. Also, in this aspect of the invention, the ester preferably will have up to about 1 free hydroxyl group per molecule.

The compositions of the invention are particularly suitable as base oils in fully formulated lubrication compositions. Thus, in another aspect of the invention, the lubricating composition herein will include at least one additive selected from antioxidants, dispersants, detergents, antiwear agents, pour point depressants, friction modifiers, viscosity modifiers and antifoaming agents.

As will be readily appreciated, the lubricating oils of the present invention make it possible to prepare lubricating compositions that have viscosities lower than the component oils but that have a Noack volatility (ASTM D 5880) and cold cranking simulator properties that are within industry standards for those parameters. Also, being able to operate an engine with a lower viscosity oil is a factor that contributes to improved engine efficiency. Thus, in one embodiment of the invention there is provided a method of improving the efficiency of an internal combustion engine lubricated with a natural or GTL oil by adding to the oil a sufficient amount of a polyol ester to provide a composition having a kinematic viscosity at 100° C. that is less than that of each of the oil and the ester at that temperature.

EXAMPLE 1

In this example a series of lubricating compositions were prepared from a polyol ester and a mixture of mineral oils. The polyol ester was a high hydroxyl ester (HHE) obtained from Exxon Chemical Co., Houston, Tex. and had about 1 hydroxyl group per molecule (corresponding to approximately 105 mg KOH/gram). The mineral oil was a mixture of MCT 10 and MCT 30, sold by Imperial Oil Co., Calgary, Canada, and the ratio was adjusted to give a similar viscosity to the HHE ester. The kinematic viscosity of the ester at 100° C. was 8.506 cSt and the kinematic viscosity at 100° C. of the MCT mixture was 8.547 cSt. The kinematic viscosity of the mixtures were determined at 100° C. and at 40° C. The results are presented in FIGS. 1 and 2. The Cold Cranking Simulator (CCS) viscosity at −10° C. was also determined (ASTM Test D5293), and the results are presented in FIG. 3. The data are also shown in Table 1.

TABLE 1 Kinematic Viscosity and CCS Viscosity Data of HHE and MCT Blends MCT HHE kV @ kV @ CCS@ Density@ wt % wt % 100° C., cSt 40° C., cSt −10° C., cP 15° C. 0 100 8.506 71.65 3790 0.9855 10 90 8.245 67.68 3360 20 80 8.091 65.43 3170 30 70 8.001 64.14 3000 40 60 7.959 63.28 2900 50 50 7.950 62.84 2790 0.9269 60 40 7.971 62.62 2660 70 30 8.018 62.57 2630 80 20 8.110 62.98 2560 90 10 8.256 64.00 2550 100 0 8.547 67.08 2630 0.8768

EXAMPLE 2

The procedure of Example 1 was followed except that the polyol had a kinematic viscosity at 100° C. of 4.008 cSt, and the oil was a GTL oil that had a kinematic viscosity of 3.724 cSt at 100° C.

The viscosity and cold cranking properties of the compositions and components are given in FIGS. 4 to 6. The data are shown in Table 2.

TABLE 2 Kinematic Viscosity and CCS Viscosity Data of HHE and GTL Blends Oil 03-33289 03-33290 03-33291 03-33292 03-33293 03-33294 Component wt % wt % wt % wt % wt % wt % HHE 100 80 60 40 20 GTL 20 40 60 80 100 KV at 100 C., cSt 4.008 3.827 3.700 3.653 3.638 3.724 KV at 40 C., cSt 19.118 17.522 16.446 15.94 15.694 16.07 CCS at −30, cSt 2353 1732 1359 1197 1038 992

EXAMPLE 3

The procedure of Example 1 was followed except that the ester was a polyol ester with a mixed alkyl groups ranging from C2 to C24, with no free hydroxyl groups and a Kv at 100° C. of 5.004. Also, the oil was a GTL oil having a Kv at 100° C. of 4.240. The viscosity properties of the components and blends are given in FIGS. 7 and 8.

EXAMPLE 4

The procedure of Example 3 was followed, but in this instance the GTL oil used had a Kv at 100° C. of 6.32 cSt. The viscosities of the components and compositions are given in FIGS. 9 and 10.

EXAMPLE 5

A preblend of Group II basestocks were prepared using 64.8 wt % 260N and 35.2 wt % 580N oils. This preblend was then mixed with a high hydroxy ester (HHE) having the properties shown in Table 3.

TABLE 3 Gp II Blend, wt % 10 90 80 70 60 50 40 30 20 10 0 HHE, wt % 0 10 20 30 40 50 60 70 80 90 100 KV@100° C., cSt 8.534 8.218 8.044 7.975 7.920 7.886 7.894 7.916 8.014 8.132 8.425 KV@40° C., cSt 65.85 62.75 61.73 61.48 61.65 62.03 62.22 62.94 64.24 66.46 70.67 CCS@−10° C., 2250 2200 2240 2330 2510 2640 2740 2870 3070 3360 3820 cP

EXAMPLE 6

Two engine oil formulations (5 W-30) were prepared using a Group III basestock P1008 obtained from PetroCanada, Calgary, Canada and the high hydroxy ester (HHE) of Example 1. The compositions are shown in Table 4.

TABLE 4 Oil 1 Oil 2 PetroCanada P1008 65.70 wt % 60.90 wt % XA 19102 (C98-148)  8.60 wt %  8.60 wt % Paratone 8451 (C96-46) 10.50 wt % 10.30 wt % Paraflow 390 (C95-090)  0.20 wt %  0.20 wt % High Hydroxy Ester 15.00 wt % 20.00 wt % (C97-189) KV@100° C., cSt 10.44 10.49 KV@40° C., cSt 59.92 60.52 CCS@−30° C., cP 3640 4240 CCS@−25° C., cP 1960 2230 MRV@−40° C., cP 24,800 36,100 MRV@−35° C., cP 10,000 12,900 MRV is the mini rotary viscometer test (ASTM D4684) XA 19102 is a detergent-inhibitor package from Oronite (Richmond, CA) Paraflow 390 is a pour point depressant package from Paramins (Linden, NJ). Paratone 8451 is a viscosity index (VI) improver from Oronite (Richmond, CA) 

1. A lubricating composition comprising: a polyol ester which is the reaction product of a neopolyol with linear or branched monocarboxylic acids, and mixtures thereof having from 1 to about 25 carbon atoms and a natural or GTL oil of lubricating viscosity and mixtures thereof; the weight ratio of ester to oil being a ratio sufficient to provide a composition having a kinematic viscosity at 100° C. that is less than the kinematic viscosity at 100° C. of each of the oil and ester.
 2. The composition of claim 1 wherein the ester has from 0 up to about 1 free hydroxyl groups.
 3. The composition of claim 1 wherein the weight ratio of ester to natural or GTL ratio is between 20:80 to 80:20.
 4. The composition of claim 2 wherein the neopolyol is selected from the group consisting of neopentylglycol, trimethylolpropane, monopentaerythritol, technical grade pentaerythritol, and dipentaerythritol.
 5. The composition of claim 4 wherein the monocarboxylic acid is a mixture of acids.
 6. The composition of claim 5 wherein the natural oil of lubricating viscosity is a mineral oil.
 7. The composition of claim 6 wherein the ester and mineral oil have substantially the same kinematic viscosity at 100° C.
 8. The composition of claim 7 wherein the mineral oil is a blend of mineral oils.
 9. The composition of claim 1 wherein the oil of lubricating viscosity is a GTL oil.
 10. The composition of claim 9 wherein the polyol ester has substantially no free hydroxyl groups.
 11. The composition of claim 9 wherein the neopolyol is pentaerythritol, and the monocarboxylic acids are a mixture of acids.
 12. The composition of claim 1, 8, and 11 including at least one additive selected from the group consisting of antioxidants, dispersants, detergents, antiwear agents, pour point depressants, friction modifiers, viscosity modifiers and antifoamants.
 13. A method for improving the efficiency of an internal combustion engine lubricated with a lubricating oil composition comprising a natural or GTL base oil, the method comprising providing the base oil with a polyol ester of a neopolyol with linear or branched monocarboxylic acids and mixtures thereof having from 1 to about 25 carbon atoms in an amount sufficient to provide a composition having a kinematic viscosity at 100° C. that is less than the kinematic viscosity at 100° C. of each of the oil and ester.
 14. The method of claim 13 wherein the ester has from 0 up to about 1 free hydroxyl group per molecule.
 15. The method of claim 14 wherein the oil is a natural mineral oil.
 16. The method of claim 14 wherein the oil is a GTL oil. 